Removal of acetylenic hydrocarbons from diolefine-containing mixtures



Patented Sept. 2, 1947 REMOVAL OF ACETYLENIO HYDROOAR- BONS FROM DIOLEFlNE-CONTAINING MIXTURES Ludo x. Frevel, Midland, Mich., assignor a. The Dow Chemical Company, Midland, Mich., a corporation of Michigan No Drawing. Application July 17, 1944, Serial No. 545,392

7 Claims. 1

This invention concerns a method and certain catalysts for the treatment of hydrocarbon mixtures comprising a dioleilne and another at least equally unsaturated hydrocarbon to hydrogenate selectively and thereby remove the latter without destruction of more than a minor amount of the diolefine. It pertains especially to such method and catalysts for the treatment of hydrocarbon mixtures comprising a conjugated diolefine to remove therefrom other hydrocarbons which are alphabeta-unsaturated and which have no hydrogen atom attached to the beta carbon atom.

It is known that dioleflnes, and particularly conjugated dioleflnes are produced in dilute form, but in large .quantities, in various processes for the pyrolysis of petroleum fractions and other hydrocarbon starting materials. The dioleflnecontaining mixtures obtained in such processes usually comprise a variety of hydrocarbons other than the diolefines, and separation of the latter in a form suitable for use in the preparation of synthetic rubber has proven difficult. For instance, cracked-oil gas, which is a well-known source of diolefines, usually comprises paraffinic hydrocarbons ranging from methane to hexane; oleflnes such as ethylene, propylene, butylenes, amylenes,

and hexenes; diolefines such as allene, butadiene- 1,3, methylallene, isoprene, and piperylene; and a small but appreciable amount of acetylenic hydrocarbons such as acetylene, methylacetylene, ethyl acetylene, and vinyl acetylene, etc. I

Although such mixture may be distilled to obtain fractions consisting for the most part of hydrocarbons having the same number of carbon atoms in the molecule and the diolefine content of each fraction may be concentrated by usual purification procedures, e. g. by extraction with solvents, the acetylenic hydrocarbons and other highly unsaturated hydrocarbon impurities of close to the same boiling point as the diolefines tend to accompany the latter during such treatments. For instance, butadiene-LB which has been recovered from cracked-oil gas by such conventional treatments usually retains a minor amount, e. g. less than 0.1 molecular equivalent, of acetylene homologues such as methyl-acetylene, ethyl-acetylene, and vinyl-acetylene, and may also retain a small but appreciable proportion of an unconjugated diolefine such as allene or methyl-allene. Such impurities are objectionable when the diolefine is to be employed in the production of synthetic rubber. Although certain treatments, e. g. with agents capable of forming metal acetylides, are known whereby the acetylenic hydrocarbons may be removed, such treatments are expensive or difllcult to carry out and are not well suited to commercial practice. Hydrogenation of the hydrocarbons with usualhydrogenation catalysts, even when carriedout using hydrogen in an amount chemically equivalent to the acetylenes, ordinarily results in de- (Cl. zoo-681.5)

struction of a considerable part of the 'diolefine. It is an object of this invention to provide a simple, inexpensive method whereby vapor mixtures comprising a dioleflne and, as an impurity incident to manufacture of the diolefline, a minor amount of an alpha-beta-unsaturated hydrocarbon containing no hydrogen atom on the beta carbon atom may be treated to hydrogenate such impurity selectively without excessive loss or destruction of the diolefine. Another object is to provide hydrogenation catalysts which are suitable for use in the process. Other objects will be apparent from the following description of the invention. I

In order to be suitable for the purpose it is imortant that the used catalyst be readily regenerated, e. g. by successive oxidation and reduction treatments, to render it again active. During use as a catalyst for the hydrogenation of hydrocarbons, a finely divided metal gradually loses its activity, e. g. because of poisoning by'the sulphur compounds usually associated with the hydrocarbons or because of accumulation on the catalyst of non-volatile organic or carbonaceous substances. The removal by oxidation of accumulated sulphur from the finely divided nickel often used as a catalyst is diflicult. Also, most finely divided individual metals, when oxidized to remove such impurities and thereafter reduced 30 with hydrogen, tend to increase in crystal size during the reduction. Such crystal growth causes a reduction in the catalytic activity.

I have found that although a conjugated diolefine such as butadiene-l.3 and alpha-beta-unsaturated hydrocarbons containing no hydrogen on the beta carbon atom, e. g. methyl-acetylene and allene, are equally unsaturated, as regards the amount of bromine which may be added to the molecule, they nevertheless differ appreciably in resistance to reaction with hydrogen. In general, I find that hydrogen may be reacted more readily with an alpha-acetylene than with an alpha-beta-diolefine, and more readily with the latter than with a conjugated diolefine. How- 4 ever, all such highly unsaturated hydrocarbons are capable of undergoing other chemical reactions, e. g. polymerization and/or carbonization.

in the presence of hydrogenation catalysts. The

hydrogenation methods and catalysts heretofore 50 known are not satisfactory for the selective hydrogenation of one such highly unsaturated hydrocarbon, e. g. an acetylene, in the presence of another, e. g. a dioleflne, without considerable destruction of the latter.

I have discovered an entire series of hydrogenation catalysts which are highly selective in causing the hydrogenation of certain highly unsaturated hydrocarbons in the presence of others and have also discovered the conditions under which 60-such catalysts may be employed to remove from a diolefine an acetylene or other alpha-beta-unsaturated hydrocarbon, e. g. allene. having no hydrogen atom on the beta carbon atom.

The new hydrogenation catalysts consist essentially of finely divided copper or iron in intimate admixture with a minor amount of one or more other finely divided metals which are themselves active hydrogenation catalysts. Peculiarly, finely divided iron or copper, although known as catalysts for other hydrogenation reactions, have not proven to be effective as catalysts for the vapor phase hydrogenation of'such highly unsaturated hydrocarbon impurities. Apparently, the temperature necessary for hydrogenation in the presence of these individual metals is above that required for decomposition of the highly unsaturated hydrocarbons. n the other hand, nickel usually causes the concurrent hydrogenation of acetylenes and dioleiines and frequently promotes thermal decomposition, e. g. carbonization of such hydrocarbons. However, by forming an intimate mixture of finely divided copper or iron with a minor amount oi? one or more other finely divided metals, the oxides of which are reducible by hydrogen at temperatures below 550 C.. there is obtained a catalyst mixture which is highly selective in action and which permits the ready hydrogenation of one unsaturated hydrocarbon in the presence of another equally unsaturated hydrocarbon that is only slightly less susceptible to hydrogenation. These particular mixtures of metals are, when necessary, readily reactivated, e. g. to remove accumulated carbon, non-volatile organic substances, or sulphur compounds, by the aforementioned successive oxidation and reduction treatments. During the step of reducing the metal oxides with hydrogen little, if any, crystal growth appears to take place. 1

For the purpose of this invention, the catalyst mixtures are prepared so as to contain between 85 and 99.9, preferably between 90 and 97, per cent by weight of one of the metals iron and copper and between 15 and 0.1, preferably between and 3, per cent of another metal, the oxide of which is reducible with hydrogen at temperatures below 550 C. Examples of metals which may be employed together with the copper or iron in forming the mixed metal catalyst are chromium, cobalt, magnanese, nickel, vanadium, titanium, molybdenum, cadmium, zinc, silver, etc., and also mixtures of such metals. Peculiarly, although each of the metals copper and iron, when used alone, is substantially inactive as a catalyst for the hydrogenation of the homologues of acetylene, either of such metal may be rendered highly effective for the purpose by having intimately admixed therewith a minor amount of the other metal.

It should be mentioned that the catalysts containing copp r as the principal metal ingredient, are not well adapted to the treatment of hydrocarbon mixtures containing an appreciable amount, e. g. more than 0.1 per cent by weight, of acetylene, C2H2, since copper, at elevated temperatures, promotes the conversion of acetylene to the solid or tarry substance known as cuprene. This restriction does not apply to the catalysts containing iron as the principal metal ingredient.

I The hydrocarbon-fractions containing diolefines are usually freed, e. g. by distillation, of acetylene prior to employment in the present process. The homologues of acetylene which are retained in such fractions may selectively be hydrogenated in the presence of any of the catalysts provided by the invention.

The catalysts are preferably employed in dispersed form on a substantially inert carrier material such as aluminum silicate, brick, stoneware, pumice, or porous silica, etc. Usually the supported catalyst is prepared so as to contain from 10 to 30 per cent by weight of the mixture of metals, but it may contain such metals in smaller or greater proportions.

The supported catalyst is ordinarily prepared by immersing the supporting material in an aqueous solution of the nitrates of the metals of which the catalyst is to be composed, thereafter removing and drying the supporting material, heating it in air to convert the metal nitrates into the corresponding oxides, and reducing the latter with hydrogen. The step of roasting to convert the metal nitrates to oxides is usually accomplished at temperatures between 550 and 700 0., preferably at GOO-650 C., but it may be carried out at somewhat lower or at higher temperatures. Reduction of the metal oxides is carried out at temperatures below 550 0., and usually between 250 and 350 0., but this step .also may be accomplished at lower or higher temperatures. Complete reduction of the metal oxides to the free metal is not in all instances necessary. For instance, when using the catalysts containing iron as the principal metal ingredient, it frequently happens that only about one-half or two-thirds of the iron oxide is reduced to the metal during the step of reducing the metal oxides with hydrogen. However, the oxides of most of the metals which may be employed as ingredients of the catalyst are readily reducible; hence, in most instances the metal oxides are reduced nearly completely to the free metals.

The supported catalysts may, if desired, be prepared in other ways. For instance, they may be prepared by immersing the supporting material in a solution of organic salts. e. g. formates or acetates, etc., of the metals to be employed as the catalyst ingredients. Either water or a volatile organic liquid such as acetic acid, acetone, or dioxane, etc., may be used as the solvent for such salts, the preferred medium' being dependent, of course, on the particular salts employed. Thereafter the supporting material may be removed from the solution and dried by evaporating the solvent. The metal salts which remain deposited on the supporting material are then oxidized, e. g. by heating in a current of air at temperatures in the order of 500-700 C., after which the residual metal oxides are reduced with hydrogen. Still other ways of forming a deposit of the finely divided and intimately mixed metals on the supporting material will be apparent.

In general, the catalysts are employed at temperatures below 300 C., and preferably below 250 C., in the treatment of diolefine-containing mixtures to remove therefrom highly unsaturated hydrocarbon impurities such as those hereinbefore mentioned. At higher temperatures, in the presence of the catalysts, diolefines undergo chemical reactions such as hydrogenation, polymerization and/or carbonization, to an objectionable extent. It will be understood that the maximum temperatures at which the catalysts may satisfactorily be used vary somewhat with the different catalysts and with changes in the rate of vapor flow, the depth of the catalyst bed, etc. In practice, the selective hydrogenation is usually carried out at temperatures below 225 C.

The minimum temperatures at which the catalysts may be-used for the selective hydrogenation, and therefore the ranges of temperatures over which they may be used, vary with changes in the kinds and proportions of the metals of which the catalysts are composed. In general,

In comparative experiments, using catalytic mixtures of copper and nickel supported on porous alpha-cristo balite, such metal mixture consisting of 99.91 per cent copper and 0.09 per cent nickel was satisfactorily active at 205 C. and above, whereas a mixture of 94.7 per cent copper and 5.3 per cent nickel was quite active at approximately 100 C. and was satisfactorily active at 135 C. Similarly, the minimum practical operating temperatures for catalytic mixtures consisting of a major amount of iron and a minor amount of copper decreased with increase in the proportion of the copper, and the minimum practical operating temperatures for mixtures consisting of a major amount of copper and a minor amount of iron decreased with increase in the proportion of the iron. However, the admixture with the copper or iron, employed as the principal catalyst ingredient, of a large proportion of another catalytic metal often results in a catalytic mixture which is not satisfactorily selective and which promotes destruction, e. g. by hydrogenation, polymerization or carbonization, of a considerable amount of the dioleflne in the hydrocarbon mixture under treatment. It is for these reasons that the catalyst is prepared so as to contain, together with the principal copper or iron ingredient, between 0.1 and 15, and preferably between 3 and 10, per cent by weight of one or more other metals.

The catalysts provided by the invention permit the selective hydrogenation of an alpha-acetylene in the presence of either a conjugated or an unconjugated diolefine, and they permit the selective hydrogenation of an alpha-beta-dioleflne, e. g. propadiene or butadiene-1.2, in the presence of a conjugated diolefine. It follows, 01 course, that they permit the concurrent hydrogenation in a single step of both an alpha-acetylene and an alpha-beta-dioleflne in the presence of a conjugated dioleflne to render the latter substantiall free of the equally unsaturated hydrocarbon impurities.

In order to hydrogenate an alpha-acetylene selectively in the presence of an alpha-beta-diolefine without appreciable destruction of the latter, it is necessary that the mixture, when passed over the catalyst, contain hydrogen in not more than per cent excess over the amount theoretically required to reduce the acetylene to a corresponding mono-oleflne. In practice the hydrogen is employed in the amount theoretically required for such reduction of the acetylene. Also, it is desirable that the reduction be carried out at a temperature not greatly in excess of that necessary for satisfactorily rapid reaction, since the tendency for the diolefine to react becomes greater with rise in the temperature. However. the

temperature may be varied considerably within the ranges hereinbefore stated, and yet obtain satisfactory results. Thus, the invention may be applied in treating a mixture of allene and methyl-acetylene to reduce and remove the latter and obtain the allene in more readily puriiiable orm.

Also, in order to hydrogenate selectively either an aipha'beta-dioleflne, or both an alpha-betadioleflne and an acetylene, in the presence of a conjugated diolefine without appreciable destruction of the latter, it is necessary that the mixture;

when passed over the catalyst, contain hydrogen in amount not exceeding by more than 10 per cent (and preferably corresponding to) that theoretically required to reduce such unsaturated hydrocarbons other than the conjugated diolefine to simple mono-oleflnes. In this instance,

also. it is desirable, but not essential, that the selective hydrogenation be carried out at a temperature not greatly higher than that necessary for satisfactorily rapid reaction.

However, in the commercial purification of dioleflns, particularly conjugated dioleiines, by the present method, it often is desirable to employ a considerable excess of hydrogen, over the amount theoretically required for reduction of the accompanying highly unsaturated hydrocarbon impurities, and to sacrifice a. minor amount of the dioleflne in order to assure substantially complete removal of the impurities. In all instances, the excess of hydrogen, over the amount required for hydrogenation of the undesired hydrocarbon impurities, is restricted so as not to exceed 10 per cent of the molecular equivalent of the diolefine which is to be purified.

In purifying a dioleflne in accordance with the invention, a hydrocarbon mixture comprising a dioleflne and one or more of the at least equally unsaturated hydrocarbon impurities hereinbefore mentioned, is treated with hydrogen in the amount stated above and vapors of the resultant mixture are passed at a reaction temperature below 300 C., and preferably below 250 C., over or through a bed of one of the aforementioned granular supported hydrogenation catalysts. If the hydrocarbon mixture under treatment comprises sulphur compounds, these preferably are removed prior to passage over the catalyst, since they tend to poison, i. e. deactivate, the latter. The sulphur compounds may be'removed in any of several known ways, e. g. by passing the vapors, at room temperature or above, through a bed of copper oxide or by scrubbing the vapors with an aqueous, or an alcoholic, solution of an alkali metal hydroxide such as sodium or potassium hydroxide, etc.

Heating of the vapors to the reaction temperature may be accomplished in any of several ways, e. g. by external heating of the bed or catalyst or by preheating the vapor mixture before passage over the catalyst. It is preferably accomplished by injecting into the vapor mixture steam which has been superheated sufliciently to bring the resultant mixture to the desired reaction temperature. The steam not only heats the reaction vapors quickly to a substantially uniform temperature, but appears also to aid in preventing the accumulation of carbon or tarry deposits on the catalyst.

However, during continued use in the process the catalyst gradually becomes less active, due apparently to an accumulation of an oily material,

presumably polymerized hydrocarbons, on the same. Usually, the catalyst may be employed continuously over a period of several days before sufllcient polymerized material is accumulated to reduce greatly its activity.

were to be absorbed on 8 a the Silocel. The solution was heated, tge'ther with the Silocel, on a steam bath for about one hour, after which unabsorbed liquor was decanted irom the Silocel and the When the catalyst becomes less active than'delatter was dried and heated at about 650 C. in sired, it is regenerated by discontinuing the now contact with air so as to convert the metal nitrates of the hydrogen and hydrocarbon mixture, sweepto. the corresponding oxides. Thegranular maing such vapors from the catalyst chamber with terial was swept free of oxygen with steam, cooled steam, and thereafter passing air, or a mixture 1 to about 320v C. and, while atapproxiznately said of steam and air, over the catalyst while heating temperature, treated with hydrogen to 'reduceithe the latter usually at temperatures of from 400? metal oxides to .the metals. Thereafter, a to 7009C. During such passage of an oxygen cracked-oil gas fraction which contained becontaining gas over the catalyst, any tarry mates tween 50 and 60 per cent by weight of butadienerials in the latter are oxidized and removed and 1.3, between 38 and 45 per cent or butylenes, and

the metals of which the catalyst is composed .are minor amounts of butanes and highly unsatuin most instances oxidized. Thereafter, th inrated hydrocarbons such as methyl-acetylene, troduction of air is discontinued, the catalyst ethyl-acetylene, and vinyl-acetylene, etc, was chamber is swept free of oxygen with steam, and passed, together with hydrogen, in about twice the metaloxides are reduced with hydrogen as the amount theoretically requiredto reduce the hereinbefore described. The catalyst is then in acetylenes t0 m noefi s. v r th ranular condition for continued use in carrying out the hydrogenation catalyst while heating the latter. selective hydrogenation reaction. 7 The granul r catalyst w s employed in the form During passagetogether with hydrogen over of a bed of, 3 centimeters diameter and 40 centi the catalyst in the manner just described, the meters depth. The vapor mixture was passed conjugated dioleflnes in a hydrocarbon mixture lengthwise through'the bed of catalyst at a rate react to only a minor extent, or not at all, but which, when expressed as'at 25 C. and atmosthe accompanying hydrocarbons of as great a de-; pheric pressure, corresponded to 625 cubic cenigree of unsaturation are almost completely hymeters per minute. ,The catalyst was heated drogenated. The diolefines thus freed. of equally initially at a temperature of about 320 C., but unsaturated hydrocarbon impurities may be sep-' during passage of the vapors over the same the arated from the mixture in any ofseveral known temperature was gradually lowered until analysis ways, e. g. by extraction with selective solvents, of the acetylenes in the mixture flowing to the or by treatment with chemical agents, such as catalyst and of the acetylenes in the vapors flowammoniacal cuprous chloride, which react to form ing from the cataly t indicated that the latter was thermally unstable addition compounds. no longer sa sf t y a t v p ration at the The following examples describe a number of thr old e per e. e. the minimum temways in which the principle of the invention has D r a hi h h c lyst was satisfactorily been applied, but are not to be construed as limactive, was continued for a time sufllcient to perm t invention mit determination of the proportion of acetylenes EXAMPLE 1 4o in'the hydrocarbon mixture being fed to the catalyst and, also, in the hydrocarbon mixture flow- In each of a series of experiments, granular ing from the catalyst. The following table gives Silocel (a porous form of silica) was immersed in the composition, in per cent by weight, of each an aqueous solution of the nitrates of metals catalyst thus tested and the threshold temperawhich were to be tested as hydrogenation catature for the catalyst. It also gives the per cent lysts. The total concentration of the metal ni-,- by Weight of acetylenes in the hydrocarbons being trates, and also their relative concentrations, were fed to the catalyst and in the hydrocarbons flowvaried from one experiment to the next in according from the catalyst when maintaining the latter ance with the proportions of the nitrates which at the threshold temperature.

' Table I Catalyst Pei Cent or acetylanes in Hydrocar- Run Catalytic Metals T lli reshold bons Flowingg p Kind Pa Gem data. 52.3%?

200 0. 2 0. 0% 205 2- 3 3g? 115 2.2 0. 0a 4 39k 13 1.93 0.020 5 3:3 200 2.2 0.014 e g 190 2.4 0.06 7 ng; 2.2 0.24 a 2.2 0.0 0 8:3 115 2.2 0.084 10 h 150' 2.20 0.014 11 Zm g v 2.2 0.024 12 3:; 230 1.9a 0.10 13 {5 3 225 2.4 0.44

1 Very 8118118 reaction.

9 I 10 Ezm'u 2 Table III-Continued A number ct catalysts were prepared and tested r cm as in Example 1. However, while operating at mm the threshold temperature, the per cent by weight a Temperature. 0. 1 Treated oi acetylenes and also or butadlene-Lli, both in m the hydrocarbon mixture being fed to the catalyst and in the hydrocarbon mixture flowing (mm 140 (m the catalyst. were determined. Table II states 8.2? the composition or each catalyst, gives the thresh- I" 110 old temperature for the catalyst, and states the W on per cent by weight of butadiene-LS and of acetylcues in the hydrocarbons present both in the This data indicates that under the conditions vapors flowing to the catalyst and in those nowemployed the threshold temperature was between in: from the catalyst. l 125 and 135 0., probably a ut 130 C.

Table II Per Oeutoillutadiene- Per Cent of Acetylene! v 1.3 in Hydrocarbons in Hydrocarbons Run Catalytic Metals l 'egzg mowing- 310M118- en W eltlh 3 3? e eelt chug? 1 81.8 33 1: 3 115 52.4 61.5 a1 0.024 a 87.1' gggg g 135 62-9 51.4 as 0.03 a 14.0 fla g 2:2 140 52.4 52.0 a1 0.01s 4 77.6 ggggg 142 oas 49.4 1.5 0.01s 5 86.7 w at- I: t; 193 5&0 I 58.0 act 0.014

Exam 3 m 4 The purpose or this example is to present data so A vaporized cr ck di 8 ra ti n. 11- collected duringanexperiment tor the determinataming approximately 5 3 per cent by weight 0! tion of the threshold temperature or a hydrobutadiene-L3, per cent or butylenes. 4 per genation catalyst. The catalyst wasone concent of butanes, 2 per cent of acetylene comslsting or 78.7 per cent by weight of Silocel, 20.6 pounds such as methyl-acetylene, ethyl-acetylene p r cent p r P cent n e el- I 40 and vinyl-acetylene, and a minor amount of was pr p r d as described in Example 1. The sulphur compounds, was treated with 4 per cent granular catalyst was employed in the form of by volume of hydrogen. The mixture was passed a bed of 3 centimeters diameter and-40 centlat room temperature first through a bed of meters depth. A cracked-oil gas fraction having Aseame di hydrgxlde and asbestos the composition stated in Example 1 and consure) d tha through b d of granular cum-1c t inins ppr m 2 P cent y weight of oxide tor the purpose or removing the sulphurae ty was admixed with 4 P r cent 01 its containing impurities. The gasilowing from the volume of hydre n- The mixture was passed latter bed was passed at a rate of 520 cubic centit a rate o 624 P r m e (when expressed meters per minute through a heated bed of 138 as at 25 C. nd ne m p r Pressure) grams or a granular catalyst which had been through the catalyst bed while heating the latter prepared as deserlbed in Example 1 and hi i iti y at a t mp f 1 During consisted or '78.: per cent by weight or Sllocel, a e f the V p Over the catalyst, the r- 20.6 per cent of copper and 0.7 per cent of nickel. eture was gradually lowered and the P cent During the experiment, the temperature of the by weight of acetylenes in the hydrocarbon flow- 5 catalyst bed was raised gradually fro t ing from the catalyst was determined at each of a C and the percent by weight of the acety number of different temperatures. The lowest lenes remaining m the hydrocarbons flowing temperature at which the catalyst was highly effrom the bed was tam/fined at each a mum tective in causing hydrogenation of the acetylenes her of dm t temperatures The values was considered to be the "threshold temperature." so termmed were;

Table III states the temperature for each measurement of the concentration or acetylenes in the Table IV hydrocarbons flowing from the catalyst and gives the value determined. a Tm m Redd! Table 111 o lzer t(hint oi 32 ce enes Temperature, C. in Tzilted 0.03.

. Hydrocarm5 Do.

bons 70 When the temperature had been brought to 205 0., a sample of the hydrocarbons flowing from the bed of catalyst was analyzed to determine 7 the proportions of the different kinds of hydrocarbons present. It was found to have the composition:

' Percent Butadiene-1.3 a 51.8

Butylenes 44.5

Butanes 3.7

Acetylenes 0.04

EXAMPLE 'A vaporized cracked-oil gas fraction having the composition given in the following table was admixed with 4.68 per cent of its volume of hydrogen and the mixture was scrubbed at room temperature with an aqueous sodium hydroxide solution of 15 per cent concentration in order to remove the sulphur-containing impurities. The gaseous mixture was dried by pasasge through a bed of flaked sodium hydroxide. It was then passed at a rate (expressed as at 25 C. and atmospheric pressure) of 2.617 liters per minute through a heated bed of a granular hydrogenation catalyst which was composed of approximately. 80 per cent by weight of Silocel, 19 per cent of copper and 1 per cent of nickel and which had been prepared as described in Example 1. The catalyst bed was of 3 centimeters diameter and 40 centimeters length. It contained 185 grams of the catalyst. During passage of the gases over the catalyst, the latter was heated at temperatures of from 145 to 173 C. The hydrocarbon mixture which had been passed over the heated catalyst was collected and analyzed. The following table gives the analysis of the hydrocarbon mixture both before and after the treatment.

It will benoted that the methyl-acetylene was completely hydrogenated, whereas a considerable portion of the propadiene was not reduced. Apparently, the nitrogen and oxygen in the treated mixture had been introduced during collection of the sample for analysis.

The method and catalysts herein described have also been employed in freeing the conjugated diolefines, i. e. isoprene and piperylene, in the C5 fraction of cracked-oil gas of other hydrocarbons of as great or greater degree of unsaturation. In this instance, the highly unsaturated hydrocarbons which are removed by selective hydrogenation include acetylenic hydrocarbons such as ethyl-acetylene, vinyl-acetylene, pentynes and possibly hexynes.

Other modes of applying the principles of the invention may be employed instead of those explained, change being made as regards the method or catalysts herein disclosed providing the steps or ingredients stated by any of the follow ing claims or the equivalent of such stated steps I or ingredients be employed.

I therefore particularly point out and distinctly claim as my invention:

12 1. A method of treating a vaporized hydrocarbon mixture comprising a diolefine and a diiferent alpha-beta-unsaturated hydrocarbon,

having no hydrogen atom, on the beta carbon suflicient also to reduce as much as 10 per cent of the diolefine over. a granular catalyst consisting essentially of between and 99.9 per cent by weight of copper intimately admixed with between 15 and 0.1 per cent of a different metal, the oxide of which is reducible to the metal with hydrogen at temperatures below 550 0., both of said metals being dispersed on an inert porous supporting material, while heating the vapors in the presence of the catalyst at a reaction temperature below 300 C.

2. The method, as described in claim 1, wherein the catalyst consists essentially of an intimate mixture of between and 97 per cent of finely divided copper and between 10 and 3 per cent of a different finely divided metal, the oxide of which is reducible to the metal by hydrogen at temperatures below 550 C.

3. The method, as described in claim 1, wherein the reaction vapors are passed over the catalyst while at a reaction temperature between 100 and 250 C. and the catalyst consists essentially of an intimate mixture of between 90 and 97 per cent by weight of finely divided copper and between 10 and 3 per cent of a difierent finely divided metal, the oxide of which is reducible to the metal by hydrogen at temperatures below 500 C.

4. A method, as described in claim 1, wherein hydrogen is employed in an amount sufficient to reduce the acetylene but insuflicient also to re-- duce as much as 10 per cent of the butadiene-LS, and during contact with the catalyst the reaction vapors are heated at a reaction temperaturebetween 100 and 250 C.

5. In a method of treating a fraction of cracked-oil gas, which comprises a conjugated diolefine and a minor amount of a diiferent but at least equally unsaturated hydrocarbon having no hydrogen on the beta carbon atom and that tends to distill. together with the conjugated diolefine, to remove said unsaturated hydrocarbon other than the conjugated diolefine, the steps of treating the vaporized mixture with hydrogen in amount suflicient to reduce the hydrocarbon other than the conjugated diolefine which is as unsaturated as the latter but in amount insufiicient also to reduce as much as 10 per cent of the conjugated diolefine, passing the resultant mixture at a reaction temperature between 100 and 250 C. over a hydrogenation catalyst consisting essentially of a dispersion on an inert porous material of between 90 and 97 partsby below 550 C., the

13 weight of finely divided copper intimately admixed with between 10 and 3 parts of a different finely divided metal, the oxide of which is reducible to the metal by hydrogen at temperatures below 550 C.

6. The method, as described in claim 5, wherein the hydrocarbon mixture is rendered substantially free of sulphur compounds before being passed over the catalyst.

7. In a method of treating a fraction of cracke oil gas, which fraction comprises a conjugated diolefine and a minor amount of a difierent, but at least equally unsaturated hydrocarbon, having no hydrogen on the beta carbon atom, that tends to distill together with the conjugated diolefine, and which fraction is substantially free of acetylene and sulphur compounds, to remove from the fraction said unsaturated hydrocarbon other than the conjugated dioleflne, the steps of treating the vaporized mixture with hydrogen in amount sufllcient to reduce the hydrocarbon other than the conjugated dioleflne which is as unsaturated as the latter, but in amount insufllcient also to reduce as much as 10 per cent of the 14- conjugated diolefine, and passing the resultant mixture at a reaction temperature between 100 and 250 C. over a hydrogenation catalyst consisting essentially of an intimate mixture of between 90 and 97 parts by weight of finely divided copper and between 10 and 3 parts of finely divided nickel, the mixture of these metals being supported on an inert porous material.

LUDO K. FREVEL.

REFERENCES CITED The following references are of record in the file of this patent:

UNITED STATES PATENTS OTHER REFERENCES Article in J. A. C. S., vol. 64, pages 363 to 368- February 1942, by Thompson et al. 

